CA2872273C - Process and apparatus for producing synthesis gas - Google Patents
Process and apparatus for producing synthesis gas Download PDFInfo
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- CA2872273C CA2872273C CA2872273A CA2872273A CA2872273C CA 2872273 C CA2872273 C CA 2872273C CA 2872273 A CA2872273 A CA 2872273A CA 2872273 A CA2872273 A CA 2872273A CA 2872273 C CA2872273 C CA 2872273C
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- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 33
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 112
- 239000007789 gas Substances 0.000 claims abstract description 69
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 64
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 37
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 35
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 21
- 239000007858 starting material Substances 0.000 claims abstract description 21
- 239000000446 fuel Substances 0.000 claims abstract description 14
- 238000010304 firing Methods 0.000 claims abstract description 10
- 238000000629 steam reforming Methods 0.000 claims abstract description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 13
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 13
- 239000001257 hydrogen Substances 0.000 claims description 12
- 229910052739 hydrogen Inorganic materials 0.000 claims description 12
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 8
- 239000003463 adsorbent Substances 0.000 claims description 7
- 238000005194 fractionation Methods 0.000 claims description 4
- 239000003345 natural gas Substances 0.000 claims description 4
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 2
- 125000004043 oxo group Chemical group O=* 0.000 claims 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 9
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- 230000000274 adsorptive effect Effects 0.000 description 5
- 239000001569 carbon dioxide Substances 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0415—Purification by absorption in liquids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
- C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/046—Purification by cryogenic separation
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0495—Composition of the impurity the impurity being water
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1258—Pre-treatment of the feed
Abstract
The invention relates to a process and an apparatus for producing synthesis gas (5) by steam reforming, in which nitrogen is separated off from a starting material (1) containing hydrocarbons and nitrogen in order to produce a low-nitrogen feed (4) for a burner-fired steam reformer (D), with formation of a hydrocarbon-containing residual gas (2) which subsequently serves as fuel (6). The characterizing feature here is that the nitrogen is separated off adsorptively (N) from the starting material and the hydrocarbon-containing residual gas (2) is used for firing the steam reformer (D).
Description
Description Process and apparatus for producing synthesis qas The invention relates to a process for producing synthesis gas by steam reforming, in which nitrogen is separated off from a starting material containing hydrocarbons and nitrogen in order to produce a low-nitrogen feed for a burner-fired steam reformer, with formation of a hydrocarbon-containing residual gas which subsequently serves as fuel.
The invention further provides an apparatus for carrying out the process of the invention.
In the following, the term synthesis gas is used to refer to gas mixtures which consist predominantly of hydrogen and carbon monoxide but also contain water and carbon dioxide (002). Especially carbon monoxide, hydrogen and/or a gas mixture consisting of hydrogen and carbon monoxide, known as oxo gas, are obtained as products from the synthesis gas by purification and fractionation and these are used in manifold ways in industry.
For the purposes of the present invention, the term low-nitrogen refers to a feed for a steam reformer when its nitrogen content does not exceed a value of 3% by volume.
Under industrial conditions, cryogenic processes are mostly used for separating the two synthesis gas components hydrogen and carbon monoxide. A prerequisite for the applicability of these processes is that the stream fed to the cryogenic gas fractionator used for carrying out the process is free of water, carbon dioxide and other materials which would lead to solids formation and thus to deposits at the low temperatures which occur. The synthesis gas is therefore firstly subjected to a multistep purification in which the major part of the materials which are undesirable in the cryogenic gas fractionator is removed in a CO2 scrub. The synthesis gas is freed of the remaining residues in an adsorber station downstream of the CO2 scrub.
Particularly when carbon monoxide having a purity of more than 99 mol% is to be obtained as product, the removal of nitrogen introduced with the synthesis gas into the cryogenic gas fractionator requires a considerable outlay in terms of apparatus and Date Recue/Date Received 2021-07-06 P130170-DE = IC0597 26.11.2013 - Werner Fischer
The invention further provides an apparatus for carrying out the process of the invention.
In the following, the term synthesis gas is used to refer to gas mixtures which consist predominantly of hydrogen and carbon monoxide but also contain water and carbon dioxide (002). Especially carbon monoxide, hydrogen and/or a gas mixture consisting of hydrogen and carbon monoxide, known as oxo gas, are obtained as products from the synthesis gas by purification and fractionation and these are used in manifold ways in industry.
For the purposes of the present invention, the term low-nitrogen refers to a feed for a steam reformer when its nitrogen content does not exceed a value of 3% by volume.
Under industrial conditions, cryogenic processes are mostly used for separating the two synthesis gas components hydrogen and carbon monoxide. A prerequisite for the applicability of these processes is that the stream fed to the cryogenic gas fractionator used for carrying out the process is free of water, carbon dioxide and other materials which would lead to solids formation and thus to deposits at the low temperatures which occur. The synthesis gas is therefore firstly subjected to a multistep purification in which the major part of the materials which are undesirable in the cryogenic gas fractionator is removed in a CO2 scrub. The synthesis gas is freed of the remaining residues in an adsorber station downstream of the CO2 scrub.
Particularly when carbon monoxide having a purity of more than 99 mol% is to be obtained as product, the removal of nitrogen introduced with the synthesis gas into the cryogenic gas fractionator requires a considerable outlay in terms of apparatus and Date Recue/Date Received 2021-07-06 P130170-DE = IC0597 26.11.2013 - Werner Fischer
2 energy. In the prior art, nitrogen is therefore separated off from the starting material containing hydrocarbons and nitrogen by distillation in a cryogenic process so that the synthesis gas produced in the steam reformer is low in nitrogen. Such a process is described, for example, in the patent document EP0983218B1, in which the synthesis gas obtained by steam reforming is fed to a hydrocarbon synthesis. In order to prevent poisoning of the catalyst used in the hydrocarbon synthesis, nitrogen is separated off cryogenically from a hydrocarbon-containing starting material, giving a nitrogen-rich, hydrocarbon-containing residual gas which is subsequently used as fuel.
However, the high costs incurred for the cryogenic removal of nitrogen, which considerably impair the economics of the process, are a disadvantage here.
The adsorptive removal of nitrogen from hydrocarbon-containing mixtures, in particular from natural gas, has been prior art for some years. Here, the gas mixture to be purified is passed through a vessel filled with a specific adsorbent. While the nitrogen present in the gas mixture is retained by the adsorbent, the major part of the hydrocarbons can be taken off again from the vessel. As soon as the adsorbent is saturated with nitrogen, the gas flow is interrupted and the adsorbent is regenerated, with the pressure in the vessel being below ambient pressure. The flushing gas enriched with desorbed materials (mostly nitrogen but also hydrocarbons) finally leaves the vessel as residual gas. Compared to the separation by distillation, the adsorptive removal of nitrogen can be carried out at considerably lower costs but a disadvantage is the comparatively low yield of the process which has hitherto ruled out its use in the treatment of feeds for steam reforming.
It is therefore an object of the present invention to provide a process and an apparatus of the type described at the outset which make it possible to overcome the above-described disadvantages of the prior art.
According to the invention, the stated object is achieved in terms of the process by the nitrogen being separated off adsorptively from the starting material and the hydrocarbon-containing residual gas being used for firing the steam reformer.
The process of the invention makes it possible to cover all or at least part of the fuel required for firing the steam reformer by residual gas from the adsorptive removal of nitrogen, so that, in the most favourable case, the importation of additional fuel can be P130170-DE = IC0597 26.11.2013 -Werner Fischer
However, the high costs incurred for the cryogenic removal of nitrogen, which considerably impair the economics of the process, are a disadvantage here.
The adsorptive removal of nitrogen from hydrocarbon-containing mixtures, in particular from natural gas, has been prior art for some years. Here, the gas mixture to be purified is passed through a vessel filled with a specific adsorbent. While the nitrogen present in the gas mixture is retained by the adsorbent, the major part of the hydrocarbons can be taken off again from the vessel. As soon as the adsorbent is saturated with nitrogen, the gas flow is interrupted and the adsorbent is regenerated, with the pressure in the vessel being below ambient pressure. The flushing gas enriched with desorbed materials (mostly nitrogen but also hydrocarbons) finally leaves the vessel as residual gas. Compared to the separation by distillation, the adsorptive removal of nitrogen can be carried out at considerably lower costs but a disadvantage is the comparatively low yield of the process which has hitherto ruled out its use in the treatment of feeds for steam reforming.
It is therefore an object of the present invention to provide a process and an apparatus of the type described at the outset which make it possible to overcome the above-described disadvantages of the prior art.
According to the invention, the stated object is achieved in terms of the process by the nitrogen being separated off adsorptively from the starting material and the hydrocarbon-containing residual gas being used for firing the steam reformer.
The process of the invention makes it possible to cover all or at least part of the fuel required for firing the steam reformer by residual gas from the adsorptive removal of nitrogen, so that, in the most favourable case, the importation of additional fuel can be P130170-DE = IC0597 26.11.2013 -Werner Fischer
3 dispensed with entirely. The residual gas can thus be utilized as material of value within the production of synthesis gas, as a result of which the disadvantage of the low yield of the adsorptive removal of nitrogen is largely overcome and the advantage of lower costs is almost fully brought to bear.
If the amount of the residual gas obtained in the adsorptive removal of nitrogen exceeds the amount of fuel required for firing the steam reformer, the excess amount is usefully exported as fuel and, for example, used for firing an adjacent steam reformer.
Advantageous embodiments of the process of the invention provide for carbon monoxide and/or hydrogen and/or oxo gas to be obtained as gas product from the synthesis gas produced.
Preference is given to using natural gas as starting material containing nitrogen and hydrocarbons.
The process of the invention allows gas products such as carbon monoxide and/or oxo gas to be obtained in high purity from the synthesis gas produced, and additional removal of nitrogen can in the most favourable case be omitted entirely.
Should it nevertheless be necessary to remove nitrogen from the synthesis gas, this can be carried out with a comparatively low outlay.
Furthermore, the invention provides an apparatus for producing synthesis gas having a burner-fired steam reformer and also a facility for producing a low-nitrogen feed for the steam reformer from a starting material containing hydrocarbons and nitrogen, which is connected via a line to a burner in such a way that a hydrocarbon-containing residual gas obtained in the removal of nitrogen from the starting material can be fed as fuel by the line to the burner.
In terms of an apparatus, the stated object is, according to the invention, achieved by the facility for producing a low-nitrogen feed comprising an adsorber for separating off nitrogen from the starting material containing nitrogen and hydrocarbons, which is connected to a burner for firing the steam reformer via a line in such a way that hydrocarbon-containing residual gas obtained in the adsorber can be fed as fuel via the line to the burner.
P130170-DE = 100597 26.11.2013 -Werner Fischer
If the amount of the residual gas obtained in the adsorptive removal of nitrogen exceeds the amount of fuel required for firing the steam reformer, the excess amount is usefully exported as fuel and, for example, used for firing an adjacent steam reformer.
Advantageous embodiments of the process of the invention provide for carbon monoxide and/or hydrogen and/or oxo gas to be obtained as gas product from the synthesis gas produced.
Preference is given to using natural gas as starting material containing nitrogen and hydrocarbons.
The process of the invention allows gas products such as carbon monoxide and/or oxo gas to be obtained in high purity from the synthesis gas produced, and additional removal of nitrogen can in the most favourable case be omitted entirely.
Should it nevertheless be necessary to remove nitrogen from the synthesis gas, this can be carried out with a comparatively low outlay.
Furthermore, the invention provides an apparatus for producing synthesis gas having a burner-fired steam reformer and also a facility for producing a low-nitrogen feed for the steam reformer from a starting material containing hydrocarbons and nitrogen, which is connected via a line to a burner in such a way that a hydrocarbon-containing residual gas obtained in the removal of nitrogen from the starting material can be fed as fuel by the line to the burner.
In terms of an apparatus, the stated object is, according to the invention, achieved by the facility for producing a low-nitrogen feed comprising an adsorber for separating off nitrogen from the starting material containing nitrogen and hydrocarbons, which is connected to a burner for firing the steam reformer via a line in such a way that hydrocarbon-containing residual gas obtained in the adsorber can be fed as fuel via the line to the burner.
P130170-DE = 100597 26.11.2013 -Werner Fischer
4 The adsorber is usefully filled with an adsorbent which is able to adsorb predominantly nitrogen from the starting material and desorb it again at a reduced pressure.
The facility for producing a low-nitrogen feed preferably has an adsorber station in which a plurality of adsorbers as are known from the prior art are connected to one another in such a way that both the low-nitrogen feed and the hydrocarbon-containing residual gas can be obtained as a continuous stream.
The invention further provides for the apparatus of the invention to be connected via a line to a fractionation facility in which oxo gas and/or carbon monoxide and/or hydrogen can be obtained as product from the synthesis gas.
In the following, the invention is illustrated by means of an example shown schematically in Figure 1.
Figure 1 shows an apparatus according to the invention for producing low-nitrogen synthesis gas from which a plurality of gas products are obtained in a downstream fractionation facility.
A starting material containing hydrocarbons and nitrogen, for example natural gas, is introduced via line 1 into a facility T in order to obtain a low-nitrogen feed 4 for the steam reformer D. In the facility T, the starting material 1 firstly goes into the adsorber station N in which nitrogen is separated off adsorptively from the starting material 1, giving a residual gas 2 containing nitrogen and hydrocarbons and also a low-nitrogen hydrocarbon stream 3. To separate off one or more further materials, for example sulphur, the low-nitrogen hydrocarbon stream 3 is fed into the separation apparatus S
from which a hydrocarbon-rich stream 4 is taken off and introduced as feed into the reformer tubes R of the burner-fired steam reformer D where it is converted with the aid of a catalyst together with steam in an endothermic reaction into a synthesis gas 5 which contains hydrogen, carbon monoxide, carbon dioxide and also water and is low in nitrogen. In order to obtain the heat required for steam reforming, a part 6 of the residual gas 2 containing nitrogen and hydrocarbons is fed to the burner B
arranged in the firing space F of the steam reformer D and burnt. Residual gas 7 which is not P13C170-DE = IC0597 26 11.2013 -Werner Fischer required for heating the steam reformer D is exported as fuel and, for example, used for heating a steam reformer operated in parallel (not shown).
Water is condensed out of the synthesis gas 5 in the cooler W before the synthesis gas
The facility for producing a low-nitrogen feed preferably has an adsorber station in which a plurality of adsorbers as are known from the prior art are connected to one another in such a way that both the low-nitrogen feed and the hydrocarbon-containing residual gas can be obtained as a continuous stream.
The invention further provides for the apparatus of the invention to be connected via a line to a fractionation facility in which oxo gas and/or carbon monoxide and/or hydrogen can be obtained as product from the synthesis gas.
In the following, the invention is illustrated by means of an example shown schematically in Figure 1.
Figure 1 shows an apparatus according to the invention for producing low-nitrogen synthesis gas from which a plurality of gas products are obtained in a downstream fractionation facility.
A starting material containing hydrocarbons and nitrogen, for example natural gas, is introduced via line 1 into a facility T in order to obtain a low-nitrogen feed 4 for the steam reformer D. In the facility T, the starting material 1 firstly goes into the adsorber station N in which nitrogen is separated off adsorptively from the starting material 1, giving a residual gas 2 containing nitrogen and hydrocarbons and also a low-nitrogen hydrocarbon stream 3. To separate off one or more further materials, for example sulphur, the low-nitrogen hydrocarbon stream 3 is fed into the separation apparatus S
from which a hydrocarbon-rich stream 4 is taken off and introduced as feed into the reformer tubes R of the burner-fired steam reformer D where it is converted with the aid of a catalyst together with steam in an endothermic reaction into a synthesis gas 5 which contains hydrogen, carbon monoxide, carbon dioxide and also water and is low in nitrogen. In order to obtain the heat required for steam reforming, a part 6 of the residual gas 2 containing nitrogen and hydrocarbons is fed to the burner B
arranged in the firing space F of the steam reformer D and burnt. Residual gas 7 which is not P13C170-DE = IC0597 26 11.2013 -Werner Fischer required for heating the steam reformer D is exported as fuel and, for example, used for heating a steam reformer operated in parallel (not shown).
Water is condensed out of the synthesis gas 5 in the cooler W before the synthesis gas
5 goes via line 8 into the carbon dioxide removal A, for example an aMDEA
scrub. Here, carbon dioxide is separated off to form a gas mixture 9 which consists largely of carbon monoxide and hydrogen and is conveyed further into the cryogenic gas fractionator CB.
In the cryogenic gas fractionator CB, which is configured without nitrogen removal, oxo gas 10 and also carbon monoxide 11 can be produced as products having a high purity because of the substantial absence of nitrogen in the synthesis gas 5. The hydrogen-rich stream 12 is introduced into the pressure swing adsorber DWA in order to obtain a high-purity hydrogen product 13 by removal of impurities.
scrub. Here, carbon dioxide is separated off to form a gas mixture 9 which consists largely of carbon monoxide and hydrogen and is conveyed further into the cryogenic gas fractionator CB.
In the cryogenic gas fractionator CB, which is configured without nitrogen removal, oxo gas 10 and also carbon monoxide 11 can be produced as products having a high purity because of the substantial absence of nitrogen in the synthesis gas 5. The hydrogen-rich stream 12 is introduced into the pressure swing adsorber DWA in order to obtain a high-purity hydrogen product 13 by removal of impurities.
Claims (8)
1. A process for producing synthesis gas by steam reforming, wherein nitrogen is separated off from a starting material containing hydrocarbons and nitrogen in order to produce a low-nitrogen feed for a burner-fired steam reformer, with formation of a hydrocarbon-containing residual gas which subsequently serves as fuel, wherein the nitrogen is separated off adsorptively from the starting material and the hydrocarbon-containing residual gas is used for firing the steam reformer.
2. The process according to Claim 1, wherein residual gas not required for firing the steam reformer is exported as fuel.
3. The process according to Claim 1 or 2, wherein one or more of carbon monoxide, hydrogen, and oxo gas is obtained as gas product from the synthesis gas produced.
4. The process according to any one of Claims 1 to 3, wherein natural gas is used as starting material containing nitrogen and hydrocarbons.
5. An apparatus for producing synthesis gas having a burner-fired steam reformer and also a facility for producing a low-nitrogen feed for the steam reformer from a starting material containing hydrocarbons and nitrogen, which is connected via a line to a burner in such a way that a hydrocarbon-containing residual gas obtained in the removal of nitrogen from the starting material is fed as fuel by the line to the burner, wherein the facility for producing the low-nitrogen feed comprises an adsorber for separating off nitrogen from the starting material containing nitrogen and hydrocarbons, which is connected to the burner for firing the steam reformer via the line in such a way that the hydrocarbon-containing residual gas obtained in the adsorber is fed as fuel via the line to the burner.
6. The apparatus according to Claim 5, wherein the adsorber is filled with an adsorbent which is able to adsorb predominantly nitrogen from the starting material containing nitrogen and hydrocarbons and desorb nitrogen again when the adsorbent is flushed with a low-nitrogen, hydrocarbon-containing gas.
7. The apparatus according to Claim 5 or 6, wherein the adsorber is part of an adsorber station wherein a plurality of adsorbers are connected to one another in such a way that both the low-nitrogen feed and the hydrocarbon-containing residual gas is obtained as a continuous stream.
8.
The apparatus according to Claim 5, wherein the apparatus is connected to a fractionation facility wherein one or more of carbon monoxide, hydrogen, and oxo gas is obtained as gas product from the synthesis gas.
The apparatus according to Claim 5, wherein the apparatus is connected to a fractionation facility wherein one or more of carbon monoxide, hydrogen, and oxo gas is obtained as gas product from the synthesis gas.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102013020343.0A DE102013020343A1 (en) | 2013-12-03 | 2013-12-03 | Process and apparatus for syngas production |
| DEDE102013020343.0 | 2013-12-03 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2872273A1 CA2872273A1 (en) | 2015-06-03 |
| CA2872273C true CA2872273C (en) | 2022-05-17 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2872273A Active CA2872273C (en) | 2013-12-03 | 2014-11-25 | Process and apparatus for producing synthesis gas |
Country Status (4)
| Country | Link |
|---|---|
| US (1) | US9365783B2 (en) |
| CA (1) | CA2872273C (en) |
| DE (1) | DE102013020343A1 (en) |
| RU (1) | RU2674427C2 (en) |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6136222A (en) * | 1991-12-11 | 2000-10-24 | Bend Research, Inc. | Liquid absorbent solutions for separating nitrogen from natural gas |
| US5852061A (en) | 1997-05-06 | 1998-12-22 | Exxon Research And Engineering Company | Hydrocarbon synthesis with cryogenic nitrogen removal upstream of the syngas generation |
| JP4533515B2 (en) * | 2000-08-16 | 2010-09-01 | 三菱重工業株式会社 | Syngas production method |
| DE102006019699A1 (en) * | 2006-04-27 | 2007-10-31 | Linde Ag | Steam generation in steam reforming processes |
| EP2049437A2 (en) * | 2006-07-11 | 2009-04-22 | Shell Internationale Research Maatschappij B.V. | Process to prepare a synthesis gas |
| FR2914396A1 (en) * | 2007-03-30 | 2008-10-03 | Inst Francais Du Petrole | NEW VAPOREFORMING OVEN USING POROUS BURNERS |
| US8529663B2 (en) * | 2007-05-18 | 2013-09-10 | Exxonmobil Research And Engineering Company | Process for removing a target gas from a mixture of gases by swing adsorption |
-
2013
- 2013-12-03 DE DE102013020343.0A patent/DE102013020343A1/en not_active Ceased
-
2014
- 2014-11-25 CA CA2872273A patent/CA2872273C/en active Active
- 2014-12-02 RU RU2014148574A patent/RU2674427C2/en active
- 2014-12-03 US US14/559,309 patent/US9365783B2/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| RU2014148574A3 (en) | 2018-07-10 |
| CA2872273A1 (en) | 2015-06-03 |
| US9365783B2 (en) | 2016-06-14 |
| RU2674427C2 (en) | 2018-12-07 |
| RU2014148574A (en) | 2016-06-27 |
| US20150151963A1 (en) | 2015-06-04 |
| DE102013020343A1 (en) | 2015-06-03 |
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